Method and installation for regulating the modifier level in chromatography or supercritical extraction with recycling

ABSTRACT

A chromatography or supercritical extraction method is disclosed, in which the eluent comprises a mixture of a fluid and a modifier and in which the fluid is recycled. One exemplary method comprises an operation consisting in determining at least one quantity linked to the level of modifier that is mixed with the recycled fluid and, if necessary, a correction operation in order to limit variations in the level of modifier in the eluent at the inlet of the column or the extractor. The disclosure also relates to a chromatography or extraction installation.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a 371 filing of International application no.PCT/FR2006/001946 filed Aug. 11, 2006.

FIELD OF THE INVENTION

In general, this present invention concerns the methods that make use ofa fluid in a supercritical state and, in particular, the field ofchromatography and extraction in the supercritical phase.

SUMMARY OF THE INVENTION

More precisely, according to a first of its aspects, the inventionconcerns a chromatography or extraction method that includes:

-   -   a separating operation in a column or extractor, with the said        column or the said extractor receiving a product and being fed        into an eluent that includes a supercritical fluid, routed via a        first pumping operation, and a modifier, routed via at least one        second pumping operation,    -   an operation to collect at least one fraction downstream of the        column or extractor,    -   an operation for recycling the supercritical fluid mixed with a        residual quantity of modifier following after the collecting        operation and preceding the first pumping operation, with the        said first pumping operation being used to pumps at least the        said supercritical fluid mixed with a residual quantity of        modifier, and    -   a condensing operation, following on from the collecting        operation and preceding the first pumping operation.

Such a chromatography or extraction method, in which the supercriticalfluid is recycled, is known to those skilled in the art.

Recycling of the supercritical fluid is preferable in order to reducethe cost of implementing the method and the necessary actions,particularly when high flows are employed.

For example, at a flow of carbon dioxide (CO₂), used as a supercriticalfluid, of 80 ml/min, about 115 kg of CO₂ is lost every 24 hours if it isnot recycled. This loss represents a considerable cost.

In a conventional chromatography or extraction method in thesupercritical phase, the addition of a modifier is often necessary inorder to increase the polarity of the supercritical fluid.

In chromatography and extraction, the modifier level at the input to thechromatography column or the extractor is an important parameter thataffects the performance of the method.

When the supercritical fluid is not recycled, this modifier level iseasily kept constant in that it depends on the flow in the pumpsupplying the modifier, as well as on the flow in the pump supplying thesupercritical fluid, with these two flows themselves being keptconstant.

On the other hand, when the supercritical fluid is recycled followingthe collecting operation, a certain quantity of modifier can also be so.The result is a variation of the modifier level at the input to thecolumn or extractor, which is harmful to the method.

In chromatography, for example, a variation of the modifier level at theinput to the column affects the retention time, the resolution, andsometimes the selectivity of the eluted products and therefore thestability of the method.

This also applies to the extraction, in which the modifier level affectsthe extraction time and the concentration of extracted product.

One is familiar with French patent FR 2 601 883, which concerns a methodand a device for separation with the aid of a supercritical fluid, inwhich the supercritical fluid is recycled.

After the separating operation and before it is recycled, thesupercritical fluid, in the gaseous or semi-gaseous phase and containinga residual quantity of modifier, is brought into contact with themodifier in the liquid phase in a conventional gas/liquid contactor.

The composition of the phase with the lowest density (gaseous orsemi-gaseous) is adjusted by varying the pressure and the temperature soas to obtain the desired supercritical-fluid/modifier mixture at theoutput from contactor.

This method is limited however, due to the thermodynamic balances to beobserved in the contactor, at mixtures containing at most 10% by weightof modifier.

Moreover, this method is complex to implement. In fact it leads to arequirement for a certain number of elements in, and in relation to thecontactor, such as a system for filling and monitoring the level ofmodifier, a coating, a sintered material and a droplet-separatingdevice.

In this context, the aim of this present invention is to propose achromatography or extraction method in which the supercritical fluid isrecycled, and free of the limitations of the prior art.

To this end, the method of the invention, which also conforms to thegeneric definition provided in the foregoing preamble, is essentiallycharacterised in that it also includes:

-   -   downstream of the collecting operation and upstream of the        separating operation, an operation for determining at least one        magnitude associated with the level of modifier mixed with the        recycled supercritical fluid, and if necessary    -   an operation for correcting the flow in the first pumping        operation and the flow in the second pumping operation, in order        to limit variation, during execution of the method, of the        modifier level in the eluent at the input to the column or        extractor, and in a direction that is suitable for meeting a        first setpoint, determined beforehand, of total flow        corresponding to the sum of the flows of the first pumping        operation and the second pumping operation.

The invention therefore has the advantage of proposing controlling ofthe modifier level at the input to the column or extractor. As aconsequence, the method of the invention is more stable than the methodsof the prior art that use a modifier and recycle the supercritical fluidwithout regulation of the modifier level. By the stability of the methodis meant the maintenance of all of its parameters (temperatures,pressures, flows, levels, etc.) at constant values. In particular, themethod of the invention ensures minimal variation of the modifier levelat the input to the column or extractor.

In addition, in the method of the invention, there exists no limitationof the modifier level in the eluent. The user can choose to make up aneluent containing between 0 and 100% of modifier.

In general, an eluent constitutes the mobile phase of a chromatographyor extraction. According to the invention, the mobile phase is based ona fluid chosen from any fluid that is compatible with an application inchromatography or extraction in the supercritical phase. Hereinafter,such a fluid will be referred to as a supercritical fluid, even if, incertain pressure and temperature conditions, the fluid is not in asupercritical state in the strict sense of the term. The supercriticalstate corresponds to a pressure value (P) that is greater than thecritical pressure (Pc), and to a temperature value (T) that is greaterthan the critical temperature (Tc). Also in the supercritical state isincluded the subcritical state for which P>Pc and T<Tc. We speak of asupercritical or subcritical fluid with reference to a fluid of whichthe density and therefore the solvent power undergo wide variation withthe pressure and the temperature when it is pure.

By simplification, we refer to the supercritical or subcritical state asthe state that the fluid would assume is it were in the quoted pressureand temperature conditions only, even if, in these conditions, it ismixed with another solvent and the state of the mixture is notnecessarily supercritical or subcritical.

We finally speak of a recycled supercritical fluid even if the fluid inthe temperature and pressure conditions is not in a supercritical statein the strict sense of the term, but in a state that can be gaseous(with the temperature being greater than the liquid-vapour equilibriumtemperature for the pure fluid at a working pressure less than thecritical pressure) or liquid (with the temperature being less thanliquid-vapour equilibrium temperature for the pure fluid at a workingpressure less than the critical pressure).

The eluent can also include a liquid solvent or a mixture of liquidsolvents, which constitutes a modifier. The modifier can be an organicsolvent. This is added in order to modify the polarity of thesupercritical fluid.

By a magnitude associated with the modifier level is meant any magnitudefrom which the value of the modifier level can be obtained, directly orindirectly. Thus, this magnitude can be the modifier level itself.

In a first preferred embodiment of the invention, the operation fordetermining at least one magnitude associated with the level of modifiermixed with the recycled supercritical fluid takes place upstream of thefirst and second pumping operations and includes:

-   -   an operation for measuring, at one measuring point at least, the        density of the recycled supercritical fluid mixed with a        residual quantity of modifier, and    -   an operation for evaluating the level of modifier mixed with the        recycled supercritical fluid, with the modifier level being        evaluated, from the measured density, by means of a        calibration-density=f (modifier level) graph established        beforehand at the pressure and the temperature existing at the        measuring point and around the latter, and    -   the correction operation consists of modifying the flow in the        first pumping operation and the flow in the second pumping        operation in order to meet the first setpoint and a second        setpoint, set beforehand, for the modifier level in the eluent.

In this first embodiment, the first pumping operation and the secondpumping operation preferably take place in parallel with each other. Thesecond pumping operation can also take place upstream of the firstpumping operation.

According to a second preferred embodiment of the invention, theoperation for determining a magnitude associated with the modifier levelin the eluent consists of measuring the density of the eluent upstreamof the first pumping operation and downstream of the second pumpingoperation, and the correction operation consists of modifying the flowin the first pumping operation and the flow in the second pumpingoperation in a direction that is suitable for meeting the first setpointand a third setpoint, set beforehand, for the density of the eluent.

Preferably, the operation for determining at least one magnitudeassociated with the level of modifier mixed with the recycledsupercritical fluid is effected downstream or upstream of the condensingoperation.

Advantageously, the method of the invention can also include at leastone operation for regulating the pressure followed by at least oneoperation for regulating the temperature, downstream of the separatingoperation and upstream of the collecting operation.

The invention also concerns a chromatography or extraction installationthat includes:

-   -   a separating device such as one or more chromatography columns        or an extractor, which receives a product and feeds into an        eluent that includes a supercritical fluid, routed via a first        pump, and a modifier, routed via at least one second pump,    -   a device for collecting at least one fraction of the product        separated in the separating device,    -   a path for recycling the supercritical fluid mixed with a        residual quantity of modifier, downstream of the collection        device and upstream of the first pump, with the said first pump        pumping at least the said supercritical fluid mixed with a        residual quantity of modifier, and    -   a condenser placed downstream of the collection device and        upstream of the first pump,

with the said installation being characterised in that it also includesa measuring and correcting device, placed in the recycling path ordownstream of the first pump, and upstream of the separating device,which measures at least one magnitude associated with the level ofmodifier mixed with the recycled supercritical fluid and that, ifnecessary, performs correction of the flow in the first pump and of theflow in the second pump in order to limit the variations, while runningthe installation, of the said levels at the input to the separatingdevice, and in a direction that is suitable for meeting a firstsetpoint, determined beforehand, of total flow corresponding to the sumof the flows in the first pump and in the second pump.

According to a first preferred embodiment of the invention, themeasuring and correcting device is positioned at a measuring pointlocated upstream of the first and second pumps and measures the densityof the recycled supercritical fluid, mixed with a residual quantity ofmodifier, from which it evaluates the level of modifier mixed with therecycled supercritical fluid by means of a pre-established density=f(modifier level) calibration curve at the pressure and the temperatureexisting at the measuring point and around the latter; and the saidmeasuring and correcting device modifies the flow in the first pump andthe flow in the second pump in order to attain the first setpoint and asecond setpoint, set beforehand, of modifier level in the eluent.

In this first embodiment, the first pump and the second pump arepreferably mounted in parallel with each other. The second pump can alsobe positioned upstream of the first pump.

According to a second preferred embodiment of the invention, themeasuring and correcting device measures the density of the eluentupstream of the first pump and downstream of the second pump, and thecorrection consists of modifying the flow in the first pump and the flowin the second pump in a direction that is suitable for meeting the firstsetpoint and a third setpoint, set beforehand, for the density of theeluent. The measuring and correcting device can be located downstream orupstream of the condenser.

According to one particular embodiment, the installation according tothe invention also includes a device to regulate the pressure, apressure-reducer for example, followed by a device to regulate thetemperature of the eluent, by heating it for example, downstream of theseparating device and upstream of the collection device.

The invention is advantageously implemented with carbon dioxide as thesupercritical fluid.

As the modifier, it is preferable to use an organic solvent liquid, likean alcohol for example.

BRIEF DESCRIPTION OF THE DRAWINGS

Other characteristics and advantages of the invention will emerge moreclearly from the detailed description provided below, purely as a guideand in no way limiting, with reference to the appended drawings inwhich:

FIG. 1 is a diagram of one embodiment of the method of the invention,

FIG. 2 represents a density=f (modifier level) calibration curve thatcan be used in accordance with the invention, and

FIGS. 3 and 4 each represents a diagram of an installation according tothe invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

According to one particular embodiment of the invention, thechromatography or extraction method includes the operations representedin FIG. 1.

Conventionally, a separating operation 1 takes place in a chromatographycolumn or in an extractor.

The column or the extractor are supplied with an eluent that includes asupercritical fluid and a modifier.

The product P is inserted into the chromatography column, by injectionfor example.

A first pumping operation 2 brings the supercritical fluid, which hasbeen subjected beforehand to a condensing operation 6, to the column orto the extractor.

A second pumping operation 3 brings the modifier to the column or to theextractor.

Thus, a supercritical-fluid/modifier mixture constituting the eluent isformed for the separating operation 1. At this stage, the eluent ispreferably in a supercritical state.

An operation 11 for regulating the temperature of the eluent can beeffected before the separating operation 1. For example, the eluent isheated in a heat exchanger.

An operation 4 for collecting at least one fraction of the product P iseffected downstream of the column or extractor.

An operation 9 for regulating the pressure and an operation 10 forregulating the temperature of the eluent are preferably effectedfollowing the separating operation 1 and prior to the collectingoperation 4.

The operation 9 for regulating the pressure consists, for example, ofreducing pressure in the eluent enriched with at least one fraction ofthe product P, to a pressure that is less than the critical pressure ofthe supercritical fluid. If the supercritical fluid CO₂, the pressurereduction therefore occurs at a pressure that is less than 74 bars, andtypically between 30 and 65 bars.

After the pressure reduction, the supercritical fluid is in liquid andgaseous form. The liquid part is in the majority, and depends on thepressure at which pressure reduction takes place.

This liquid part can be converted to a gas by heating during theoperation 10 for regulating the temperature.

This conversion results in a drop in the density of the supercriticalfluid and therefore in the solubility of the solute constituting thefraction of product P in this fluid. The solubility of the solutediluted in the modifier becomes almost zero, which allows separation ofthe solute, solid or liquid, of the supercritical fluid brought to thegaseous state, by means of gas-solid or gas-liquid separators.

An operation 5 for recycling the supercritical fluid brought to thegaseous state and mixed with a residual quantity of modifier follows onfrom the collecting operation 4 and precedes the first pumping operation2.

There exist two causes for the presence of a residual quantity ofmodifier in the supercritical fluid brought to the gaseous statefollowing the collecting operation 4.

Firstly, the modifier has a vapour tension that results in a certainsolubility in the supercritical fluid brought to the gaseous state. Thepercentage of modifier that is recycled depends on the solubility of themodifier in the supercritical fluid brought to the gaseous state, andthis solubility is a function of the pressure and temperature of thesupercritical fluid brought to the gaseous state in the separators.

Secondly, the percentage of modifier that is recycled depends on theeffectiveness of trapping in the separators.

The condensing operation 6 follows on from the collecting operation 4and precedes the first pumping operation 2. It takes placeadvantageously during the recycling operation 5.

The pressure and the temperature of the supercritical fluid mixturebrought to the gaseous-modifier state, obtained by the correspondingregulating operations 9, 10, are constant during the collecting andrecycling operations 4, 5 and up to the condensing operation 6, duringwhich the temperature is lowered.

In addition, the method of the invention includes, downstream of thecollecting operation 4 and upstream of the separating operation 1, anoperation 7 for determining at least one magnitude associated with themodifier level mixed with the supercritical fluid recycled and broughtto the gaseous or liquid state.

Preferably, in order to facilitate the implementation of the method, theoperation 7 is effected upstream of the first pumping operation 2. Thefact of measuring the density at the input to the pump facilitates theoperation since, at this stage of the method, it is possible, whateverthe operating conditions of flow, column type and size, temperature,etc., to maintain a constant pressure and temperature during executionof the method and from one method to the next.

If necessary, an operation 8 for correcting the flow in the firstpumping operation 2 and the flow in the second pumping operation 3 iseffected in order to limit the variations, during execution of themethod, of the modifier level in the eluent at the input to the columnor the extractor. The flows are corrected in a direction that issuitable for meeting a first setpoint, determined beforehand, of thetotal flow corresponding to the sum of the flows of the first pumpingoperation 2 and of the second pumping operation 3.

More particularly, FIG. 1 represents an advantageous version of theinvention. According to this version, the operation 7 for determining atleast one magnitude associated with the level of modifier mixed with thesupercritical fluid brought to the liquid state takes place upstream ofthe first and second pumping operations 2, 3. It includes an operation,at one measuring point at least, for measuring the density of thesupercritical fluid recycled and brought to the liquid state, mixed witha residual quantity of modifier, and an operation for evaluating thelevel of modifier mixed with the supercritical fluid, with the modifierlevel being evaluated, from the measured density, by means of adensity=f (modifier level) calibration curve established beforehand atthe pressure and the temperature existing at the measuring point andaround the latter. Such a calibration curve is represented in FIG. 2.

The correction operation 8 consists, in this case, of modifying the flowin the first pumping operation 2, and the flow in the second pumpingoperation 3, in order to satisfy the first setpoint and a secondsetpoint, set beforehand, of modifier level in the eluent.

The density of the supercritical fluid, mixed with a residual quantityof modifier, is the sum of the densities of the constituents, namely thesupercritical fluid and modifier, weighted by their percentage, with anoffset in the case where the mixture of the constituents has a finalvolume other than the sum of the initial volumes of the constituents.

In FIG. 2, the term “density” refers to the mass per volume. Moreover,the CO₂ is given by way of an example of a supercritical fluid.

In order to draw a calibration curve as represented in FIG. 2, thedensity of the supercritical fluid mixed with a residual quantity ofmodifier, shown on the ordinate, is measured for different modifierlevels, shown on the abscissa. The different supercriticalfluid-modifier mixtures are created by the first and second pumpingoperations, at a given temperature and pressure.

The variation in the density of the supercritical fluid mixed with aresidual quantity of modifier as a function of the modifier leveldepends on the difference in density of the pure constituents in the setconditions of pressure and temperature. The greater this difference, thegreater too is the variation in the density of the mixture as a functionof its composition, and the greater is the precision in determining themodifier level.

Therefore, it is preferable to establish conditions of temperature andpressure at which the difference in density of the pure constituents isgreatest.

The precision in determining modifier level also depends on theprecision of the test gear for measuring the density.

The density=f (modifier level) curve is linear, except in the casementioned previously in which the supercritical-modifier fluid mixturehas a final volume that is different from the sum of the initial volumesof supercritical fluid and modifier.

In the configuration of the invention represented in FIG. 1, the firstpumping operation 2 and the second pumping operation 3 take place inparallel with each other.

Nevertheless, a configuration in which the second pumping operationtakes place upstream of the first pumping operation also forms part ofthe invention.

It is preferable to measure the density in order to determine the levelof modifier mixed with the supercritical fluid, in that this measurementis relatively easy to implement and has good precision, but otherphysical magnitudes can also be used to obtain the value of the level ofmodifier mixed with the supercritical fluid. It is possible, forexample, to measure the thermal conductivity of the mixture, or indeedto perform a measurement of the absorption of this melange in theultraviolet range.

According to another advantageous version of the invention, theoperation for determining a magnitude associated with the level ofmodifier mixed with the supercritical fluid recycled and brought to theliquid state, consists of measuring the density of the mixture, which isthen the eluent, upstream of the first pumping operation and downstreamof the second pumping operation. In this case, the correction operationconsists of modifying the flow in the first pumping operation and theflow in the second pumping operation in a direction that is suitable formeeting the first setpoint and a third setpoint, set beforehand, for thedensity of the eluent.

As before, it is possible to replace the measurement and the densitysetpoint of the eluent with a measurement and a setpoint of thermalconductivity or absorption in the ultraviolet.

In this configuration, one is not seeking to determine the residualmodifier level in the supercritical fluid recycled and brought to theliquid or gaseous state, but to aim for a density setpoint at the inputto the pump. For this, a regulation loop is created.

The density setpoint is determined, for example, by measuring thedensity corresponding to the modifier level in the eluent in the absenceof recycling, by adjusting the flows of the pumping operations to as toascertain the wanted modifier level and the total flow, in fixedoperating conditions.

The regulation loop consists of adjusting the flows of the pumpingoperations in the direction that is suitable to satisfy two setpoints,namely density and total flow. A single pair of values of the flows inthe first and second pumping operation satisfy both a density setpointand to a total-flow setpoint.

Advantageously, the operation 7 for determining at least one magnitudeassociated with the level of modifier mixed with the supercritical fluidis effected downstream of the condensing operation 6. In fact, in orderto measure the density, the supercritical fluid is preferably brought tothe liquid state by cooling it to below the liquid-vapour equilibriumtemperature, at the recycling pressure that is less than the criticalpressure. Thus, the measurements are more precise than measurements in agaseous phase.

Nevertheless, this operation for determining at least one magnitudeassociated with the level of modifier mixed with the recycledsupercritical fluid can be performed upstream of the condensingoperation 6. In this case, the density is measured in the supercriticalfluid brought to the gaseous state.

One way of measuring the density is, for example, the use of a massflowmeter based on the Coriolis principle, which can be used to obtainthe flow and the density, or of an appliance dedicated to the specificmeasurement of the density of a fluid or of a mixture of fluids at agiven pressure and temperature.

The measured density can be corrected to take account of thetemperature.

The supercritical fluid is preferably carbon dioxide, but can be anyfluid that is compatible with chromatography and/or extraction in thesupercritical phase, such as an alkane, a chloro-fluoroalkane or xenon.

The modifier is preferably an alcohol, like methanol, ethanol orisopropanol for example, but can also be any organic solvent, such asacetonitrile, methyltertbutylether or MTBE, or ethyl acetate. It can bea mixture of at least two of these compounds.

FIGS. 3 and 4 each schematically represent an installation according tothe invention, which can be used to implement the method of theinvention. We have chosen in particular to illustrate the chromatographyinstallations.

The same elements making up the installation are each indicated by thesame reference in these two figures.

FIG. 3 illustrates a first configuration according to the invention.This installation includes a separating device that includes at leastone chromatography column 12.

This column 12 receives a mixture that includes a product P introducedby injection and an eluent that includes a supercritical fluid, such asthe CO₂, and a modifier. The supercritical fluid, held in recipient A,is routed via a first pump 13 and the modifier, held in recipient B, isrouted via at least one second pump 14.

At the output from the column 12, a detector 20 is used to detect thefraction or fractions of the product, (P) that come out of the columnwith the eluent.

These fractions are collected in a collection device 15 that includes atleast one solid-gas or liquid-gas separator according to which thesolute constituting the fraction of product (P) is solid or liquid.Several separators can be connected in series.

In the case of an eluent that is free of modifier and that is thereforea pure supercritical pure, its recycling would simply require arrangingfor the trapping of all the solute in the separator or separators.

In the case of the invention, the eluent includes modifier at between 0and 100% by weight, preferably between 0.1% and 70%, or preferablybetween 0.5% and 35%. At the output from the column 12, there is amixture of eluent and solute, making a mixture of threeconstituents—supercritical fluid, modifier and solute.

This mixture is put through a device to regulate the pressure, and adevice to regulate the temperature. Thus, in a first stage, the mixturepasses through a pressure-reducer 19 in order to reduce the pressure ofthe eluent. This results in a mixture of supercritical fluid brought tothe liquid state, supercritical fluid brought to the gaseous state,modifier, and solute.

This last mixture is then heated in the device to regulate thetemperature, in order to convert the supercritical fluid part brought tothe liquid state into supercritical fluid brought to the gaseous state.One is therefore in the presence of two phases, namely a liquid phasecontaining the modifier in which the solute is soluble, and a gaseousphase of supercritical fluid brought to the gaseous state in which wefind a certain modifier level and traces of solute.

A first separator is used to separate the liquid phase from the gaseousphase and to collect the soluble solute in the modifier.

The use of a second separator in series with the first allows all of thesolute to be trapped.

A path 16 for recycling the supercritical fluid brought to the gaseousand then the liquid state mixed with a residual quantity of modifier ispositioned between the collection device 15 and the first pump 13. Thefirst pump 13 pumps at least the supercritical fluid brought to theliquid state and mixed with a residual quantity of modifier.

The pumped mixture first passes via a condenser 17 placed downstream ofthe collection device 15 and upstream of the first pump 13. Thecondenser 17 is preferably placed in the recycling path 17.

The installation according to the invention also includes a measuringand correcting device 18, placed in the recycling path 16 or downstreamof the first pump 13 and upstream of the chromatography column 12. Themeasurements are facilitated in the case where the device 18 is locatedin the recycling path 16, upstream of the first pump 13.

This device 18 measures at least one magnitude associated with the levelof modifier mixed with the recycled supercritical fluid and, ifnecessary, performs correction of the flow in the first pump 13 and ofthe flow in the second pump 14 in order to limit the variations, whilerunning the installation, of this level at the input to thechromatography column 12.

The correction is effected in a direction that is suitable for meeting afirst setpoint, determined beforehand, of total flow. The total flowcorresponds to the sum of the flows in the first pump 13 and in thesecond pump 14. Preferably, the measuring and correcting device 18 isplaced downstream of the condenser 17.

Nevertheless, the measuring and correcting device can also be placedupstream of the condenser.

In the first particular configuration represented in FIG. 3, themeasuring and correcting device 18 is placed at a measuring pointlocated upstream of the first and second pumps 13, 14, and moreprecisely the first pump 13 and the second pump 14 are mounted inparallel with each other.

According to a second particular configuration (not shown) of theinvention, the second pump is positioned upstream of the first pump, andthe measuring and correcting device is positioned at a measuring pointlocated upstream of the second pump.

In this case, the installation has the advantage of requiring only ahigh-pressure pump, which is the first pump 13. The second pump 14, inseries with and upstream of the first pump 13, can be just alow-pressure pump. For example, the first pump has a feed pressure ofbetween 30 and 300 bars, preferably between 100 and 300 bars, and thesecond pump, for example, has a feed pressure of between 1 and 100 bars,preferably of the order of 50 bars.

At the measuring point, in these two configurations, the measuring andcorrecting device 18 measures a first magnitude associated with themodifier level mixed with the supercritical fluid recycled and broughtto the liquid state, which is preferably the density of the mixture.From this measured density, the device 18 evaluates a second magnitudeassociated with the level of modifier mixed with the supercritical fluidrecycled and brought to the liquid state, which is the modifier level,by means of a calibration curve such as that represented in FIG. 2.

The measuring and correcting device 18 modifies the flow in the firstpump 13 and the flow in the second pump 14 in order to attain the firstsetpoint and a second setpoint, set beforehand, of modifier level in thesupercritical-fluid/modifier mixture.

The setpoints are set by the user as a function of the process that hewishes to execute with the installation according to the invention.

The recycled supercritical fluid contains traces of modifier due to thesolubility of the latter in the supercritical fluid brought to thegaseous state.

The first pump 13 pumps supercritical fluid brought to the liquid stateand containing modifier, and the flow of supercritical fluid is lessthan its initial value, meaning than the value set at the start-up ofthe installation. It is therefore necessary to increase the flow in thefirst pump 13 in order to adjust the flow of supercritical fluid to itsinitial value by compensating for the presence of the modifier.

For example, at the start-up of the installation, the flow ofsupercritical fluid is set to a value of 80 g/min, and the flow ofmodifier to a value of 20 g/min. The first total-flow setpoint istherefore 100 g/min, and the user fixes the second setpoint of modifierlevel at 20%.

The residual level of modifier in the recycled supercritical fluid is 5%for example. In this case, if the flow is not corrected in the firstpump 13, then the actual flow of supercritical fluid will be 95% of 80g/min, which is 76 g/min.

It is then necessary to adjust the flow in the first pump 13 so as tosatisfy the relation Q×0.95=80 g/min, where Q is the value of thecorrected flow in the first pump 13. Here, Q is about 84.2 g/min. Theflow in the first pump 13 is therefore increased by 4.2 g/min.

The flow in the second pump 14 is reduced so as to maintain a modifierlevel of 20% in the eluent, and a total flow of 100 g/min. The correctedflow in the second pump 14 is 100−84.2 or 15.8 g/min, which represents areduction in the initial flow of 84.2×0.05 g/min which is about 4.2g/min.

According to a third particular configuration of the invention, asrepresented in FIG. 4, the measuring and correcting device 18 measuresthe density of the eluent upstream of the first pump 13 and downstreamof the second pump 14. In other words, this third configuration differsfrom the previous two in that the second pump 14 is installed upstreamof the device 18.

In this third configuration, the correction consists of modifying theflow in the first pump and the flow in the second pump in a directionthat is suitable for meeting the first setpoint and a third setpoint,set beforehand, for the density of the eluent.

This third setpoint can be determined by the user by calculation, giventhat the density of the supercritical-modifier fluid mixture is equal tothe sum of the respective densities of the supercritical fluid andmodifier, weighted by their respective percentages, but a more precisemeasurement is preferred, by measuring in the installation in operationwithout recycling.

For regulating the flows of the two pumps 13, 14, each of these pumps isconnected to a flowmeter.

For example, an eluent is composed of CO₂, as the supercritical fluid,and ethanol as the modifier. For a pressure of 50 bars and a temperatureof 0° C., the density of the CO₂ is 950 kg/m³, and that of the ethanolis 789 kg/m³. For precision in the measurement of the density of ±0.1kg/m³, it is possible to adjust the composition of the CO₂-ethanoleluent with a precision of ±0.05%.

The precision increases as the respective densities of the supercriticalfluid and modifier differ from reach other. For example, in the casewhere the supercritical fluid is CO₂, the alcohols are very suitable asmodifiers, in that they are of low density, and the chlorated solventsare also suitable in that they are high density.

Naturally however, the chromatography column 12 can be replaced byseveral chromatography columns or, in the case of one method ofextraction, by an extractor in which we find the product P.

This column 12 can be one that contains a stationary phase like thatused in chromatography in the gaseous phase, or a column containing astationary phase like that used in chromatography in the liquid phase,such as high-performance liquid chromatography (HPLC), or indeed anyother column compatible with the separation to be effected.

Likewise, the extractor used in the invention can have a liquid or solidstationary phase.

The invention claimed is:
 1. A chromatography or extraction installationincluding: a separating device such as one or more chromatographycolumns (12) or an extractor, which receives a product (P) and feedsinto an eluent that includes a supercritical fluid, routed via a firstpump (13), and a modifier, routed via at least one second pump (14), adevice (15) for collecting at least one fraction of the product (P)separated in the separating device, a path (16) for recycling thesupercritical fluid mixed with a residual quantity of modifier,downstream of the collecting device (15) and upstream of the first pump(13), with the said first pump pumping at least the said supercriticalfluid mixed with a residual quantity of modifier, and a condenser (17)placed downstream of the collecting device (15) and upstream of thefirst pump (13), the said installation being characterised in that itfurther includes a measuring and correcting device (18), placed in therecycling path (16) or in, downstream of the first pump (13) andupstream of the separating device, which measures at least one magnitudeassociated with the level of modifier mixed with the recycledsupercritical fluid and that, if necessary, performs correction of theflow in the first pump (13) and of the flow in the second pump (14), inorder to limit the variations, while running the installation, of thesaid levels at the input to the separating device, in a direction thatis suitable for meeting a first setpoint, determined beforehand, for thetotal flow corresponding to the sum of the flows in the first pump (13)and in the second pump (14).
 2. The installation according to claim 1,wherein the measuring and correcting device (18) is positioned at ameasuring point located upstream of the first and second pumps (13, 14)and measures the density of the recycled supercritical fluid, mixed witha residual quantity of modifier, from which it evaluates the level ofmodifier mixed with the recycled supercritical fluid by means of apre-established density=f (modifier level)calibration curve at thepressure and the temperature existing at the measuring point and aroundthe latter; and wherein the said of measuring and correcting device (18)modifies the flow in the first pump (13) and the flow in the second pump(14) in order to attain the first setpoint and a second setpoint, setbeforehand, of modifier level in the eluent.
 3. The installationaccording to claim 2, wherein the first pump (13) and the second pump(14) are mounted in parallel with each other.
 4. The installationaccording to claim 2 wherein the second pump (14) is positioned upstreamof the first pump (13).
 5. The installation according to claim 1,wherein the measuring and correcting device (18) measures the density ofthe eluent upstream of the first pump (13) and downstream of the secondpump (14), and modifies the flow in the first pump (13) and the flow inthe second pump (14) in a direction that is suitable for meeting thefirst setpoint and a third setpoint, fixed beforehand, for the densityof the eluent.
 6. The installation according to claim 1, wherein themeasuring and correcting device (18) is placed downstream of thecondenser (17).
 7. The installation according to claim 1, wherein themeasuring and correcting device (18) is placed upstream of the condenser(17).
 8. The installation according to claim 1, further including adevice to regulate the pressure, such as a pressure-reducer for example(19), followed by a device to regulate the temperature of the eluent, byheating it for example, downstream of the separating device and upstreamof the collecting device (15).